EP1432535B1 - Method for processing waste products and corresponding processing plant - Google Patents

Abstract

Disclosed are a method for processing residual waste and other organically contaminated waste substances, and a residual waste processing plant, wherein a waste substance containing organic constituents is heated to the boiling temperature range of water in a reactor under vacuum, so that membranes of water-containing cell structures are destroyed, and the organically highly contaminated cell water may be discharged, together with the exhaust vapor.

Description

The invention relates to a method for processing of Waste according to the preamble of claim 1 and a residual waste processing plant according to the preamble of the independent claim 13.

The recovery of waste such as household waste, Commercial waste, organic waste, etc. is in the waste law of Lawmakers required and whenever possible one Waste disposal to be preferred. The waste law applies in principle for every waste owner as well as for waste disposal Corporate bodies such as cities and cleaning companies. In the Waste Act and in the Federal Emission Control Ordinance (BIMSCHV) is regulated that collecting, transporting and storing the waste in such a way and to treat that are the possibilities of Waste recycling can not be hindered. To fulfillment This duty of exploitation is material to municipalities or an energy recovery available.

By material recycling is meant the treatment of waste to a secondary raw material, which then used in the energy industry. That One understands under the production of the substitute fuel a material Recovery resulting from the direct combustion of the Waste is to be distinguished. The latter alternative is currently the most commonly used type of Waste recycling. Problematic with this thermal Utilization, however, is that prescribed by law Limit values, in particular to comply with the flue gas are, so that considerable plant-technical expenditures must be made to legal requirements to fulfill. Furthermore, there are the conventional waste incineration plants publicly in discussion, so that in the communities aspirations are present, the waste to be recycled.

In DE 196 48 731 A1 is a waste treatment process described in which organic components of a Waste fraction are washed out in a percolator and the thus biologically stabilized residue a drying is burned. This combustion takes place in a conventional waste incineration plant, so that with regard to the exhaust gases the same problems as in the present thermal utilization described above.

In DE 198 07 539 a method for thermal Treatment of residual waste described in which from the Waste through mechanical and biological treatment high calorific fraction is obtained. This heat rich Fraction is used as a substitute fuel of a combustion fed to a plant that is in energy association with a energy-intensive plant is operated. Alternatively, you can this substitute fuel also directly in the energy-intensive Plant to be used. In this known Solution is the biological stabilization by a aerobic degradation of the organics of the treated waste.

In DE 199 09 328 A1 is a method for processing disclosed by residual waste, in which this one aerobic Hydrolysis is supplied. In this aerobic hydrolysis becomes the biologically stabilized fraction in a Reactor with air and a leaching liquid (water) applied. By the action of atmospheric oxygen and the humidity set at the same time an aerobic, thermophilic heating of the mixture, so that the bio-cells broke up and the released ones transported organic substances through the washing liquid become. In this known reactor the mixture by means of a conveyor / agitator transversely to the air and leachate through the reactor guided.

This aerobic hydrolysis was demonstrated in first pilot plants excellent results, with a comparatively low device complexity, a substitute fuel which can not be eluted, is not breathable and is characterized by a high calorific value distinguished. This substitute fuel can, for example be fed to a gasification, wherein the resulting Gas then energetic or material in Power plants and cement works or in the production of Methanol or used as a reducing agent in steel mills can be.

In the above-described waste recycling method However, a high device-technical effort for Performing the aerobic hydrolysis required so that Such systems for a considerable space requirement require and on the other hand relatively expensive. So large quantities of highly polluted exhaust gases are generated, which exactly the 30th BIMSCHV a complex and costly Gas cleaning and combustion supplied Need to become.

In contrast, the invention is based on the object a process for the treatment of waste and a To provide treatment plant, through which the stabilization of residual waste with reduced process and Device-technical effort can be performed.

This object is with respect to the method by the Features of claim 1 and in terms of Processing plant by the features of claim 13 solved.

According to the invention, a thermal stabilization takes place of waste in a reactor that is approximately in the boiling range of Water is operated under vacuum. By operating in the Vacuum arise virtually no exhaust gases, with the residues as a product dry stable and hygienic handled and can be stored.

By the inventive operation of the reactor can the degradation of organic cells by the biological information compared to those described above significantly accelerate conventional percolation processes, so that only a fraction of the previous usual material throughput times is required. This makes it possible to make the reactor much more compact, wherein, according to the first preliminary experiments, the reactor volume at the same throughput only about 5% of a previous Percolator is.

By the thermal admission of the organic Ingredients of the residual waste in the boiling range of water become the membranes of water-bearing cell structures explosively destroyed and thus released organic highly contaminated cell water can leave the reactor subtracted from. By heating and vacuum action in the reactor, the ingredients are sanitized and can be handled human medically safe.

By lowering the boiling temperature by vacuum below the melting point of plastic components of the Waste material can damage the plastic parts during the Boiling extraction or boiling dry do not melt and smear inner walls of the container and thereby deteriorate the heat transfer.

In an advantageous variant of the inventive Method, the reactor is run as a boiling extractor, wherein the heated to boiling temperature residual waste with a Leaching liquid is applied, so that the organic washed out components of the residual waste become. Preliminary tests showed that in such a Siedekextraktor also in the residual waste existing nitrogen is expelled bound as ammonia. By the expulsion of ammonia is the nitrogen load of the Restmülls reduced so that in subsequent Process steps, such as a treatment organically contaminated leaching fluid in a biogas plant no denitrification needs to be done.

The proportion of organic in residual waste can be further lower, if at the boiling extraction a Siedetrocknung followed by the after the boiling extraction present thermally stabilized residual waste one inventive reactor is fed, in which case However, no leaching liquid is supplied but only a thermal stabilization by Heating the already pre-stabilized residual waste in the Boiling range under vacuum.

The effectiveness of the process is further enhanced, if the boiling dry and / or the boiling extraction a Preheating is upstream, allowing the reactor less heating energy for heating the residual waste to the Boiling temperature must be supplied.

With a suitable composition of the residual waste, it can also sufficient, the thermal stabilization alone by perform a boiling extraction or a boiling drying, preferably each a preheating stage upstream.

This preheating is preferably by an aerobic Rotting process performed. In such an aerobic Warming is a biologically produced hydrolysis which biochemically accelerates cell disruption and thereby in the washout at a subsequent Extraction or dehydration in one subsequent drying increased.

The accumulating after the boiling extractor or the drier Vapors is in an advantageous embodiment by means of a capacitor or equivalent Device cooled and thus condensed, so that the process - apart from minor leakage air - can be carried out substantially free of air.

The possibly resulting leakage air can be with minimal procedural effort in a burner burn or another treatment, for example to an exhaust air purification system.

As already mentioned, after the boiling extraction resulting organic polluted leaching a Biogas plant to be supplied.

In the biogas plant defed fermentation water is preferably as circulating or process water to the boiling reactor recycled. The biogas produced can be used to generate Process heat in the reactor or to generate electrical Energy used so that the system in the can be operated essentially energy self-sufficient.

In a preferred embodiment, the after the boiling drying present warm dry matter one supplied to the exhaust air-free cooling drying, so that through the concomitant dew point lowering the warm dry material is dehumidified again.

The basic module of the inventive waste processing plant consists in principle of a heatable, under vacuum operable reactor, which with a residual waste or material entry and a material discharge and a stirring device for conveying the residual waste and designed to introduce shear forces.

This reactor can when supplying leachate as a boiling extractor and - without leaching - as Drier be driven.

The stirring device of the reactor is preferably so executed that their stirring elements on the Innenumfangswandungen the reactor adhering material at a Turns off so that caked on the wall surfaces be avoided. By the effect of the stirring device the material is heated along the Innenumfangsflächenwandung shifted and the material entry for material discharge - and possibly in opposite Direction - transported.

The stirring device is preferably helical formed, with the screw with or without central shaft can be executed.

The drive of the stirring device is preferably with reversible direction of action executed, so that the conveying direction is reversible.

The effect of the stirring device is especially good when the stirrer is made heatable.

In a preferred embodiment, the residual waste and the leaching by a common Material input supplied.

The reactor can be very compact, if this is provided with two sections in which in each case a stirrer is arranged. These two sections can have a suitable material feed or a material recoil, so that the material is recoverable in the circulation.

In a preferred variant of the method, the thermal stabilized waste fraction fed to a press, wherein the organic water contained in the press water Components are implemented in a biogas plant.

By the above-described circulation of the at Waste processing, with biological components laden material flows can withstand even the toughest conditions Legislators, as for example in the 30. BIMSCHV are prescribed, with comparatively low Effort be met, as no expensive cleaning steps downstream of the exhaust air and the wastewater Need to become.

As an energy generator for heating the reactor, for example a burner, a gas turbine or a gas engine can be used, with the aforementioned streams, for example, in the biogas plant accumulating Biogas organic in the boilers contaminated exhaust air or when draining the waste supplied exhaust air for residue combustion becomes.

Other advantageous developments of the invention are Subject of the other dependent claims.

Figur 1 ein Verfahrensschema eines Grundmoduls zum Aufbereiten von Restmüll mit einer Siedeextrakion;

Figur 2 ein Grundmodul des erfindungsgemässen Verfahrens zur Aufbereitung von Restmüll mit einer Siedetrocknung;

Figur 3 einen Reaktor zur Verwendung in einem Verfahren gemäss der Figuren 1 und 2;

Figur 4 ein Ausführungsbeispiel des Reaktors aus Figur 1;

Figuren 5, 6, 7 Prinzipdarstellungen zum Zusammenschalten von Reaktorabschnitten für eine Siedeextraktion / Siedetrocknung und

Figur 8 ein Grundschema eines Verfahrens zum Aufbereiten von Restmüll mit einer Siedeextraktion und nachgeschalteter Siedetrocknung.

In the following preferred embodiments of the invention will be explained in more detail with reference to schematic drawings. Show it:

FIG. 1 shows a process diagram of a basic module for processing residual waste with a boiling extract;

Figure 2 is a basic module of the inventive method for the treatment of residual waste with a boiling drying;

FIG. 3 shows a reactor for use in a method according to FIGS. 1 and 2;

Figure 4 shows an embodiment of the reactor of Figure 1;

Figures 5, 6, 7 are schematic diagrams for interconnecting reactor sections for a boiling extraction / boiling and drying

8 shows a basic diagram of a method for processing residual waste with a boiling extraction and subsequent boiling drying.

• Restmüll
• Grossküchenabfälle
• Abfälle aus der Lebensmittelindustrie
• Gemüse und andere nachwachsende organische Abfallstoffe
• Klär- und Gärschlämme
• biologische Rückstände, bspw. Maischen, aus der Getränkeherstellung

Figure 1 shows a basic scheme of a minimum equipment for performing a boiling extraction process for the treatment of organically polluted waste such. B:

• residual waste
• Catering waste
• Waste from the food industry
• Vegetables and other renewable organic waste
• Sewage and fermentation sludges
• biological residues, for example mashing, from beverage production

The organically loaded substances 1 are a reactor. 2 supplied and with fresh water or circulating liquid 6 diluted. With a stirring device 8, the suspension 74 mixed and transported from waste and liquid. The heat supply to reach the Siedetemparatur via a jacket heating 4.

To speed up the heating process can also entrained steam 38 directly into the suspension 74 mitge and / or by an upstream heating stage, which is not shown here.

A substantial proportion of this residual waste consists of short-chain connections, mostly on the surface are absorbed. Will this surface of the hot Process water flows around, so are also primarily non-soluble Compounds hydrolyzed and washed out. The odor-intensive components of organic waste and the hydrolysis products are relatively soluble in water and can be washed out with the washout. With Such an extraction achieves a reduction the organics and a deodorization of the residual waste.

By operating the boiling extractor in the area of Boiling point of water under vacuum becomes the physical / chemical Effect of extraction by the increase of bacterial degradation significantly enhanced. The organic cells of the mixture are broken and cell water released and the dissolved organics through removed the washout liquid. It was found, that instead of using a boiling extractor 2 a conventional percolator, the throughput time of about two days with conventional percolators on two Reduced hours, so that the boiling extractor 2 with a much lower volume than conventional percolators can be trained to the same throughput to recycle waste.

The process heat treatment takes place via a heat generation plant 26 with which the heat energy 28 in the form of hot water, compressed hot water, thermal oil or steam 38 is produced.

As the heat generating system supplied energy 24 can be used in the process of self-produced biogas be, and / or other fossil fuels or electrical energy can be used.

When boiling in the boiling extractor 2 is by the Underpressure of the boiling point kept well below 100 ° C. and the jacket temperature 4 depending on the suspension 74 on a Temperature level adjusted so that no caking Adjust at the heating surfaces, so that the heat transfer into the suspension 74 without losses can.

Depending on the product mixture / suspension 74 may contain ingredients such as B. plastic parts and plastic films already for heating jacket or surface repairs 4 around 80 ° C begin to plasticize and the heat transfer surfaces and the stirring device 8 with a viscous Coat to coat. The negative pressure is caused by a Vacuum generator 4 produced (shown here as a vacuum pump) which by the generated negative pressure of preferably ≤ 80 mbar the boiling point in the boiling extractor 2 lowered to <60 ° C.

The outgoing via vapors 48 ingredients are in one Brüdenkondensator 66 by cooling 16 under the Dew point cooled and the exhaust gases 54 from the condensate 68th separated. The vacuum generator 40 may, as required, arranged before or after the vapor condenser 66 become.

The waste gases accumulating at the vapor condenser 54 contain leakage air and inert gas mixtures from the heated suspension 74 and amounts of residual gas from circulating water 6 of a biogas plant described in more detail below. The resulting amounts of exhaust gas are at a treated suspension amount of 1000 kg less than 1.0 m ³ and are thus extremely low, so that can be practically spoken of an exhaust-free process.

Due to the suspension temperature between> 40 ° C and <100 ° C and the acting negative pressure will be within a few Minute cell structures of the biogenic components changed, Torn membranes and thus the trapped biogenic mass made accessible to the washout process.

Also, for the digestion of difficult to access cellulose and lignin compounds by the above Temperature and vacuum action broken and as Biopotential of the following biogas plant 20 (Fermentation stage) supplied.

Depending on the temperature and heat capacity of the suspension 74 the heating time in the boiling reactor 2 is different and can also by preheating the aggregates 1 and the Process water 6 outside of the boiling reactor 2 essential be shortened.

After the circulating water / process water 6 to the Saturation enriched with dissolved organics, the Suspension 74 discharged and the thermally stabilized Substrate / water mixture 10 a dewatering device 14 supplied (shown here as Klassierpresse). In the dehydrator 14, the solid / press cake 22 from the organically enriched Process water 18 separated. The press cake 22 can then additional process steps are supplied, such. B. Composting, biological drying or a mechanical-thermal Drying as an example in the Figure 2 is shown.

The actual extraction process is input material dependent and lasts on average between a few minutes to over an hour. Due to the influence of temperature over one hour, the suspension 74 is sanitized and can after dewatering 14 and drying 42 (Figure 2) manageable, stored and be fed to further steps.

The process water 8 is advantageous in a biogas plant 20 (Figure 8) deflated in the organics portion is converted by means of methane bacteria to biogas 24, the then for power generation in the heat generation plant 26 and the gas surplus of a further utilization 103 (Figure 8) is supplied for heat and power generation.

The released fermentation water 32 (FIG. 8) leaves the Biogas plant 20 and is used as process water / circulating water 6 fed back to the boiling extractor 2.

The vapor condensates 68 contained a large part of Nitrogen compounds which are the biological anaerobic Degradation process in the fermenter 20 can inhibit. Therefore become the vapor condensates 68 together with the excess water 34 directly in a wastewater treatment 36 (Figure 8) treated and then as a purified Sewage 105 discharged into the sewer or as process water / process water 6 partly the boiling extraction process 2 supplied. By this reduction of the nitrogen before the biogas plant 20 requires the fermentation process no nitrogen sink anymore.

Thus, a method is presented in which in one Reactor 2 organically contaminated substances 1 with water 6 by Agitators 8 are mixed and transported and through Heat 4 near the boiling point of water under vacuum, the suspension 74 such is unlocked that within a few minutes Cell membranes destroyed, lignin and cellulose compounds broken up and an anaerobic fermentation process in a biogas plant 20 are made available so that the starting material 10 is thermally sanitized and after a dewatering step 14 and subsequent drying 42 (Figure 2) human medically as harmless substance mixture handled, processed and stored can.

The superiority of the inventive method can be concluded from a comparison of the boiling extraction with other processes in which the organics of Residual waste with 50% water content biogas is produced.

In the boiling extraction described above, the treatment time in the reactor 2 is max. 2 h with a circulating water amount of 10001 / kg residual waste, and the conversion to biogas in the fermenter 20 is max. 5 days. Since some pulp compounds are also degraded, the gas production is about 150Nm ³ / 1Mg residual waste. The methane content is 70%. The exhaust air amount is approx. 1.0m ³ / 1Mg residual waste. The energy expenditure amounts to approx. 5% of the energy yield with drying 15%.

In the percolation described above according to the patents EP 0876311 B1 and WO 00/27777, the treatment time in the reactor is at least 2 days with a circulating water amount of 30001 / 1Mg residual waste and the conversion to biogas in the fermenter is a maximum of 5 days. Pulp compounds are not degraded. The gas production is about 70Nm ³ / 1Mg residual waste. The methane content is 70%. The exhaust air quantity per 1 mg residual waste is about 1000m ³ .

In a residue fermentation according to the patents EP 0 476 217 B1 and EP 0192 900 B1, the treatment time in the gas reactor is at least 20 days with a circulating amount of seed sludge of 20% of the total content. Needed 25m ³ Drum / volume per 1Mg supplied residual waste. Pulp and lignin compounds are partially degraded after a journey time of 18 to 30 days. The gas production is about 100 Nm ³ / 1Mg residual waste. The methane content is 55 - 60%. The amount of exhaust air per 1Mg. Residual waste is about 8000 m ³ . Energy consumption approx. 30% of the energy yield.

Another known extraction method is the pressure-release explosion in which the tissue cells are kept mainly in the slaughter waste area in a continuous autoclave at 350 ° C and an overpressure of about 18bar two hours. After the holding time, a small amount is relaxed in blocks. Relaxation pressure destroys the cell membranes and allows the slaughterhouse waste to be fermented. The high temperatures and the holding time are mainly used to destroy the prions that cause mad cow disease (BSE). Approximately 40m ^{3 of} lavatory volume are needed per 1mg of slaughterhouse waste. Lignin compounds are only partially degraded. The gas production is about 300Nm ³ / 1Mg slaughterhouse waste. The exhaust air amount per 1Mg is about 10,000 m ³ . The energy consumption is about 50% of the energy yield.

• Restmüll,
• Ausgangsstoffgemische aus der Siedeextraktion, Perkolation
• Schlämme aus Klärwerken und Faulschlämme aus Vergärungsanlagen
• Produkte und Abfälle aus der Lebensmittelindustrie
• Produktionsschlämme aus der Farbenindustrie, Chemie und der Metallverarbeitung gezeigt.

In Figure 2, a minimum equipment for performing a vacuum boiling drying process for drying, stabilizing and sanitizing fabrics such as:

• Residual waste,
• Starting material mixtures from the boiling extraction, percolation
• Sludges from sewage treatment plants and digested sludges from digestion plants
• Products and wastes from the food industry
• Production slurries from the paint industry, chemistry and metalworking shown.

In a boiling dryer 42, the moist material 1, 22, 60th introduced and moved with a stirring device 8, mixed and transported. The heat supply to achieve the boiling temperature takes place via the jacket heating 4. The process heat treatment takes place again via the Heat generating system 26 with which the heat energy 28th in the form of hot water, compressed hot water, thermal oil or Steam is generated.

As an energy source 24, the self-produced biogas can be used in the boiling extraction process, and / or also other fossil fuels or electrical energy be used.

When boiling in the boiling dryer 42 is by vacuum the Boiling point kept well below 100 ° C and the jacket temperature 4 depending on the moisture content 1, 22, 60 to a temperature level adjusted so that no caking Adjust at the heating surfaces, so that the heat transfer entered into the moist material 1, 22, 60 without losses becomes.

The operation of the boiling dryer 42 substantially corresponds the operation of the boiling extractor shown in Figure 1 2 except that no process water 6 is supplied. For the sake of simplicity in terms of Basic functions of the Siedetrockners 42 on the corresponding References to the boiling extractor 2.

Depending on the inlet temperature and heat capacity of the Moistened material 1, 22, 60 is the heating time in the boiling dryer 42 different and may also be due to preheating of the moist material 1, 22, 60 outside the boiling dryer 42 are significantly shortened (device not shown). After heating to operating temperature takes the actual drying process depending on the humidity of the Wet material 1, 22, 60 between 1.5 to 3 hours.

By a temperature effect at more than 90 ° C over one hour hold time is the dry product 50 then sanitized and human medically safe handled, stored and fed to further operations become.

The dry product 50 leaves the boiling dryer 42 with an outlet temperature of about 60 to 80 ° C. through the symbolically shown mass flow deflection 62 can the warm dry material 50 stored or further treated become. But if for the subsequent further treatment a lower material temperature is desired is the warm dry material 50 a cooling dryer 52 fed. The cooling dryer 52 consists of a dense Housing with an internal perforated conveyor belt 56 with which the dry material 50 (cake) from the entrance is promoted to the exit.

The with heat and residual moisture from the dry material 50th laden exhaust air 78 is in a cooler / condenser 66th cooled and dehumidified. The condensate 68 is the Wastewater treatment (Figure 8) supplied. With a circulating air fan 70 becomes the cooled and dehumidified Drying air 80 through the perforated conveyor belt 56th and the material cake 50 passed. The cooled dry material 72 does not leave the cooling dryer 52 over one illustrated lock and discharge device. The air circulation 78, 80 is closed, it is practically no exhaust air volumes or exhaust gases.

FIG. 3 shows a basic module 90 of a reactor which as boiling extractor 2 or as a boiling dryer 42 usable is. In this basic module 90, both functions such as Boiling extraction 2 and boiling drying 42 carried out become. The core piece forms the soulless conveying and Recirculating spiral 82 which at the same time the stirrer function. 8 takes over. With this Umwälzspirale 82 is the content 74, 76 moved gently and by the material movement 100, 102, the heating surface 4 kept free of caking and thus the heat transfer from the heating medium 28 in the to be heated moist material or in the suspension 74 ensured.

In summary, this means that the ingredients 74, 76 in both processes 2, 42 together with the stirring movement 100, 102 of the spiral 82, the heat exchange surface of Constantly clean off reactor 2, 42 from soiling and due to the geometry of the spiral 82, 8 no Ribbons, cords or other long fiber parts or fabrics can wind up or lead to pigtails.

The recirculating spiral 82 is driven by at least one drive 96 moves and prevents a special sealing bushing 98 the entry of leakage air. About the entrance gate or the lock 84 become the aggregate materials 1, 6, 22, 60 supplied and after completion of the Cycle time via the outlet slide or the lock 88 the product 10, 50 discharged.

By the over the pumps 40, 44 (Figure 1, 2) set Vacuum becomes the boiling point in the boiling extractor 2 or boiling dryer 42 set to well <100 ° C and the Vapors 46, 48 leave via a steam dome / vapor withdrawal 94 the reactor 2, 42 (90). In the boiling extraction the Suspension 74 briefly to operating temperature heat, in addition to the jacket heating 92, 4 steam 38 are blown.

4 shows an embodiment with a Agitator 106 with central axis and overlapping Agitator blades 107 which during rotation through the ship's screw similar arrangement the heating surfaces 92nd of the reactor with the help of the moist material 76 or the suspension 74 of caking. The Agitator 106 may also be similar to agitator blades 107 as in the already known autoclave for the production from animal meal from slaughterhouse waste or disc dryers for drying sludges by a heating medium 28 are heated (not shown here).

• die Siedeextraktion gemäss Figur 1
• die Siedetrocknung gemäss Figur 2.

The above is an apparatus for performing two methods, such as:

• the boiling extraction according to FIG. 1
• the boiling drying according to FIG. 2.

These two process steps can be successively in one and the same device 90 without the Ingredients the reactor 90 between steps have to leave.

For large systems, however, it is appropriate if the Steps in two separate process containers 2, 42 performed since the processes are boiling extraction 2 and Boiling dry 42 different residence and treatment times and an intermediary Dewatering step 14 the evaporation energy expenditure reduced in energy and time.

FIGS. 5 to 6 show arrangement examples for the Boiling extraction 2 and boiling drying 42.

FIG. 5 shows a reactor 90 which is discontinuous fills 84 and unloads 88 becomes. The one to be treated Ingredient 74, 76 is by the drive 96 with agitator 106 moves back and forth (arrow 100) until the process is completed. This arrangement and Operating mode is particularly suitable for small and individual plants in which z. B. in a day shift two be driven until three passes.

FIG. 6 shows a series-connected arrangement of several reactor stages or reactor sections, in which the individual batches are continuously loaded 84, be treated and unloaded 88. So with the shift operations 102 the vacuum is maintained, the Steps separated from each other by gate valves or locks. The individual reactor sections can be in any Number 90.1 - 90.m are connected in series.

FIG. 7 shows an arrangement in which the one to be treated Ingredient 74, 76 in a closed circuit circulated. According to this embodiment, 2 approximately prallel arranged reactor sections 90.1, 90.2 connected via sliding components 104 with each other. The two reactor sections 90.1, 90.2 each have a Agitator 106 with a drive 96, wherein the conveying direction in the two sections 90.1, 90.2 opposite is executed (arrow 102).

Between the two sections 90.1, 90.2 are the Displacement components 104 are provided, via which the respective adjacent end portions of the sections 90.1, 90.2 connected to each other, so that the illustrated Recirculation results. The material to be processed is supplied via the material entry 84 and over the Material discharge 88 discharged from the reactor.

As in the arrangement of Figure 1 is here to a discontinuous operation in which but uniformed by the uniform rotation of the ingredient (with the fill level that suits the process) conveyed by the devices (90.1, 90.2, 104) become.

The arrangement shown in Figure 7 is suitable for the Throughput of large quantities, which z. B. in several Layers can be driven and used when using at least three devices with the corresponding ones Volume buffers practically in continuous operation be driven.

Figure 8 shows a combination of the boiling extraction process according to FIG. 1 and the downstream boiling-drying process according to Figure 2 in conjunction with a biogas plant 20, a wastewater treatment plant 36 and an exhaust air treatment plant 30.

The following are the combinations and links described in which in the figures 1 and 2 so far was not received.

Residual waste or other organically contaminated waste 1 can either the boiling extraction 2 or directly be fed to the drying dryer 42 for drying. Pasty or liquid slurries 60 can be used to dry the dryer 42 are fed directly or as a mixture 62 with the press cake 22 and residual waste 1 as additives or supplied as a single component.

The accumulating at the boiling dryer and the boiling extractor 2 Vapors 48, 46 are via the vacuum generator 40 a voroder nachhaltenen cooler / condenser 66 supplied in which condenses the vapors 48, 66 and of the Exhaust gas 54 are separated. The condensate 68 is a Wastewater treatment plant 36 supplied. The accumulating Exhaust gases are, depending on the composition and pollutant content an exhaust air purification 30 or for afterburning the Brennerzuluft for the heat generator 26 admixed. The organically highly stressed press water 18 off Extraction 2 is used for deforestation and biogas production 24 of the biogas plant 20 supplied. The biogas 24 can then other energy uses, such as a thermal power plant be supplied for power generation.

The defatted fermentation water 32 from the biogas plant 20th is used as process water / circulating liquid extraction 2 supplied as leaching 6 again. The excess water 34 from the biogas plant (fermentation) 20 is in the wastewater treatment 36 together with the vapor condensate 68 and treated as purified wastewater 105 led into the sewer or a receiving water.

To get the heating energy in the form of fuel save, there is a possibility that, loaded with organics Input streams 1, 60, 22 before entry into the reactors (Extractor, dryer) 90 in an intensive rotting box (Feed container) 108 by fumigation with air 110 or with technical oxygen 111 by biologically produced aerobic heating in the short term to the desired operating temperature preset. Simultaneously with the aerobic Warming is a biologically produced hydrolysis (Acidification), in which by biochemical digestion and increasing biochemical availability the subsequent treatment steps in the reactors 90 the extraction rate at extraction 2 and the dehydration is significantly increased during drying 42.

Thus, the exhaust air stream 54 to be treated as small as be held possible, especially the Fumigation with technically enriched Sauerstroff 111. The exhaust air 54 is from the feed containers (rotting boxes) 108 deducted and the above-described exhaust treatments 30, 26 supplied for Entfrachtung or combustion.

In the presented method of treatment of organic contaminated residual waste 1 and other organically contaminated Waste 22, 60 are caused by vacuum 46, 48 and warming 4, 26, 28 the water-bearing Cells of the membranes torn open so that the cell water, as in the vacuum boiling extraction process (FIG. 1) in FIG Boiling Extractor 2, within a few minutes to Leaching of the organic shares 18 is available and is converted into biogas 24 in a biogas plant 20.

The same happens during vacuum boiling drying (FIG. 2) in which the released cell water together with the free water, which adhere to the surfaces of the drying wet material 76 is due to boiling below Vacuum as vapors 46 leaves the dryer 90.

This cell disruption has been organic until now contaminated residual waste 1 and their mixtures 74, 76th implemented by the following known methods:

1. Biological digestion by acidification (hydrolysis)

• Feuchtigkeitsregulierung
• Lufteintrag
• mechanische Umwälzung

durch bakterielle Einwirkungen bei optimalen Verhältnissen der Zellaufschluss ab dem zweiten Behandlungstag beginnt und je nach Materialzusammensetzung zwischen dem dritten und fünften Tag die höchstmögliche Aufschlussrate erreicht hat.in the first phase of an aerobic composting process in which the following parameters are set, such as:

• wicking
• air entry
• mechanical circulation

due to bacterial effects at optimum conditions, cell disruption begins on the second day of treatment and, depending on the composition of the material, has reached the highest possible digestion rate between the third and fifth day.

2. Thermal-physical decomposition

By heating in an autoclave to 120 to about 350 ° C. at an overpressure from 2.0 to 15 bar with following explosive relaxation in a collecting and relaxation vessel. This process is called a pressure relaxation explosion designated. In both methods, the Cell disruption used to release the released cell water by leaching out in a biogas plant in To convert biogas. After completion of the washout process The discharge material is usually a dewatering step supplied and the residue composted and / or in a conventional thermal or biological Drying deprived of water.

Compared to the above-mentioned and already known methods 1 u. 2 arise in the boiling extraction 2 and the boiling 42 no significant exhaust air streams. The result is a maximum of 1.0 m ³ exhaust air 54 per 1000 kg of supplied product 74, 76. For the removal of water from 1000 kg via the vapors 46, 48, the thermal energy consumption is max. 150 kWh and the electrical energy consumption max 10 kWh. The gas production in the treatment of 1000 kg of residual waste is about 200 Nm ³ biogas or 1,300 kWh heat yield, depending on the organic proportion.

In the known methods 1 and 2, the highly loaded exhaust air flow is about 3000 m ³ per 1000 kg of product 74, 76th

The thermal energy consumption is at least 280 kWh and the electrical energy consumption additionally 24 kWh.

Disclosed are a method for the treatment of residual waste and other organically contaminated waste and a residual waste processing plant, in which an organic Ingredients containing waste material in a reactor under vacuum to the boiling temperature range of water is heated, so that membranes of water-bearing Cell structures destroyed and organically highly loaded Cell water with the vapor is dischargeable.

List of reference numbers :

1

Residual waste or other organically contaminated waste with a dry matter content> 30%

2

boiling extractor

4

external heating

6

Process water (fresh water or circulating water off the biogas plant)

8th

Stirring and transport device

10

thermally stabilized residual waste / water mixture

12

drainage

14

dehydrator

16

Cooling medium producers

18

organically highly loaded process water

20

biogas plant

22

press cake

24

Biogas or other energy sources

26

Wärmeerzeugungsanlage

28

thermal energy

30

exhaust air cleaning

32

fermentation water

34

Excess water

36

wastewater treatment plant

38

steam

40

Vacuum pump to boiling extractor

42

Vakuumsiedetrockner

44

Vacuum pump to boiling dryer

46

Vapors (vacuum dryer)

48

Vapors (boiling reactor)

50

dried and warm residual waste or other waste materials

52

refrigeration dryer

54

exhaust

56

Scraper floor or conveyor belt

60

Sludges and other pasty production and waste materials with a dry matter content <40%

62

Mass flow diversion / mixer

66

Vapor condenser / cooler

68

Condensate in wastewater treatment

70

circulation fan

72

dried and cold residual waste or other waste

74

Suspension [material mixture for boiling extraction (Mixture 1 and 6)]

76

Material for vacuum drying (mixture (1, 22, 60))

78

Steam-laden circulating air

80

Dehumidified cooling air

82

Conveying and circulation spiral

84

Material input with slider

86

casing pipe

88

Material discharge with slide

90

Boiling extractor and / or vacuum dryer

92

Heating jacket, heating surfaces

94

vapor draw

96

drive

98

Vacuum-tight shaft passage

100

Material feed in one direction

102

Material feed and retraction

103

Energy utilization for surplus biogas

104

Moving, unloading and loading component

105

Purified wastewater

106

agitator

107

Agitator blades

108

Feed Container / Biological Preheating

109

metering

110

air entry

111

oxygenation

Claims (32)

1. Method for processing waste substances, wherein organic constituents of the waste substances are expelled in a reactor (2, 42, 90), comprising the steps of:

   introducing the waste substances (1) into the reactor (2, 42, 90)

   heating the waste substances (1) under vacuum to a boiling temperature of water

   applying shear forces to the waste substances (1) received in the reactor (2, 42, 90) via a stirring device (106) etc.

   destroying membranes of water-containing cell structures of the organic constituents and expelling of the engendered exhaust vapor (46, 48) containing organic constituents.
2. Method in accordance with claim 1, wherein during a boiling extraction water (6) or another suitable leaching fluid is supplied to the reactor functioning as a boiling extractor (2), and a proportion of the organic constituents is washed out with the water (6) and a part of the organic constituents and/or bound nitrogen is expelled overhead with the generated exhaust vapor (48) as ammonia.
3. Method in accordance with claim 2, wherein boiling extraction is followed by a boiling drying having the features of Claim 1.
4. Method in accordance with any one of the foregoing claims, wherein a boiling drying in accordance with Claim 1 or a boiling extraction having the features of Claim 2 is preceded by a pre-heating (108) of the waste substance (1).
5. Method in accordance with claim 4, wherein the pre-heating (108) takes place through an aerobic retting process.
6. Method in accordance with any one of the foregoing claims, wherein the exhaust vapor (46, 48) is supplied to a condenser, preferably to a cooler (66).
7. Method in accordance with claim 6, wherein leaked air generated during the process is burnt in a burner (26) or supplied to a processing.
8. Method in accordance with any one of claims 2 to 7, wherein organically contaminated leaching fluid is supplied to a biogas plant (20).
9. Method in accordance with claim 8, wherein fermentation water (32) decontaminated in the biogas plant is recycled to the boiling reactor (2) as circulation or process water (6).
10. Method in accordance with claim 8 or 9, wherein the generated biogas (24) is used for generating process heat or electrical energy.
11. Method in accordance with any one of the foregoing claims, wherein subsequently to a boiling drying having the features of claim 1 a cooling drying of the warm dry matters takes place.
12. Method in accordance with claim 2 and 3, wherein the boiling drying and the boiling extraction are performed in the same reactor (2, 42, 90).
13. Processing plant for processing waste substances (1) containing organic constituents, in particular for carrying out the method in accordance with any one of the foregoing claims, including a heatable reactor (2, 42, 90) capable of being taken under vacuum to a boiling temperature of water (6) or of another leaching fluid, and having a waste substances inlet (84), a material discharge (88), a vacuum port, a heating (92), an exhaust vapor outlet (94) and a means for the introduction of shear forces, in particular a stirring mechanism (106).
14. Processing plant in accordance with claim 13, wherein the reactor is a boiling extractor (2) having a leaching fluid inlet (84).
15. Processing plant in accordance with claim 13, wherein the reactor is a boiling dryer (42) for dehydrating the waste substances.
16. Processing plant in accordance with claim 15, wherein a pre-heater (108) is arranged upstream of the boiling dryer (42).
17. Processing plant in accordance with claim 14 and 15, wherein the boiling dryer (2) and the boiling dryer (42) are formed by the same reactor (2, 42, 90).
18. Processing plant in accordance with any one of claims 14 to 18, including a biogas plant (20) for processing of the contaminated leaching water.
19. Processing plant in accordance with claim 18, including a circulation means for recycling fermentation water (32) occurring in the biogas plant (20) as process water (6).
20. Processing plant in accordance with any one of claims 15 to 19, including a cooling dryer for post-drying of the warm dry matter.
21. Processing plant in accordance with any one of claims 13 to 20, including a condenser (66) for the exhaust vapor (46,48).
22. Processing plant in accordance with any one of claims 13 to 21, wherein the stirring mechanism (106) has a stirrer through which the waste substances may be conveyed from the inlet to the outlet.
23. Processing plant in accordance with claim 22, wherein the stirring mechanism (106) has stirring members (107) through which the material may be stripped off an inner peripheral wall of the reactor (2, 42, 90).
24. Processing plant in accordance with claim 23 or 24, wherein the stirring element (107) has the form of a worm gear with or without a center shaft.
25. Processing plant in accordance with any one of claims 22 to 24, wherein the conveying direction of the stirring mechanism (106) is reversible.
26. Processing plant in accordance with any one of claims 22 to 25, wherein the stirring element (107) is heated.
27. Processing plant in accordance with any one of claims 14 to 26, wherein the waste substances inlet and the leaching fluid inlet have the form of a common inlet (84).
28. Processing plant in accordance with any one of claims 13 to 27, including a steam inlet for supplying heating steam (84).
29. Processing plant in accordance with claim 22, wherein the reactor (2, 42, 90) has at least two sections (90.1, 90.2) in which a respective stirring mechanism (106) is arranged.
30. Processing plant in accordance with claim 29, wherein the two sections (90.1, 90.2) are interconnected via shifting components (104), so that the material may be conveyed in the circulation.
31. Processing plant in accordance with any one of claims 15 to 28, wherein a classification press (14) is arranged downstream of the boiling dryer (42).
32. Processing plant in accordance with any one of claims 13 to 31, including an effluent purification plant (36) for processing effluent occurring during the process.

Images